Method for Making a Catalyst Comprising a Phosphorous Modified Zeolite and Use of Said Zeolite

ABSTRACT

A method to make a phosphorus modified zeolite can include providing a zeolite including at least one ten member ring in the structure steaming the zeolite, mixing the zeolite with one or more binders and shaping additives, and then shaping the mixture. The method can include making a ion-exchange. The shaped mixture can be steamed. Phosphorous can be introduced on the catalyst to introduce at least 0.1 wt % of phosphorus, such as be dry impregnation or chemical vapor deposition. A metal, such as calcium, can be introduced. The catalyst can be washed, calcinated, and then steamed. The steaming severity (X) can be at least about 2. The catalyst can be steamed at a temperature above 625° C., such as a temperature ranging from 700 to 800° C. The catalyst can be used in alcohol dehydration, olefin cracking, MTO processes, and alkylation of aromatics by alcohols with olefins and/or alcohols.

FIELD OF THE INVENTION

The present invention relates to a method for making a catalystcomprising a phosphorus modified zeolite and the use of said zeolite.This modified zeolite is of interest in processes wherein said zeoliteis operated in presence of steam at high temperature. By way of exampleone can cite,

the alcohol dehydration to convert at least an alcohol into thecorresponding olefin,the cracking of C4+ olefins (also known as OCP, olefins conversionprocess) to make a mixture of ethylene and propylene,the cracking of methanol or dimethylether (also known as MTO) to producelight olefins such as ethylene and propylene as well as heavyhydrocarbons such as butenes,the alkylation of aromatics by alcohols, by way of example alkylation ofbenzene or toluene with methanol, ethanol or propanol.

BACKGROUND OF THE INVENTION

An efficient catalyst is a key in industrialization of dehydration ofalcohols as well as in the other above processes. One of the earlycatalysts employed for the dehydration of ethanol was alumina. Thiscatalyst is relatively cheap but needs low space velocity, high reactiontemperature and makes a lot of ethane, which needs to be separated.Zeolites, particularly phosphated zeolites, solve a problem withcatalyst activity and provide with ethylene fraction, which is closed topolymer grade. Zeolites, particularly phosphated zeolites, solves aproblem with catalyst activity. Catalysts comprising a phosphorusmodified zeolite (the phosphorus modified zeolite is also referred asP-zeolite) are known. The following prior arts have described variousmethods to make said catalysts.

US 2006 106270 relates to the use of a dual-function catalyst system inthe hydrocarbon synthesis reaction zone of an oxygenate to propylene(OTP) process that operates at relatively high temperatures preferablywith a steam diluent and uses moving bed reactor technology. Thedual-functional catalyst system comprises a molecular sieve havingdual-function capability dispersed in a phosphorus-modified aluminamatrix containing labile phosphorus and/or aluminum anions. It isexplained that the hydrothermal stabilization effect that is observedwhen this phosphorus-modified alumima matrix is utilized is caused bymigration or dispersion of phosphorus and/or aluminum anions from thismatrix into the bound molecular sieve. These anions are then availableto repair, anneal and/or stabilize the framework of the molecular sieveagainst the well-known dealumination mechanism of molecular sieveframework destruction or modification that is induced by exposure tosteam at temperatures corresponding to those used in the OTP reactionzone and in the regeneration zone.

U.S. Pat. No. 5,231,064 is directed to a fluid catalyst comprising clayand a zeolite, at least one of which has been treated with a phosphoruscontaining compound, for example ammonium dihydrogen phosphate orphosphoric acid, and which is spray dried at a low pH, preferably lowerthan about 3. Said catalysts are deemed to advantageously exhibitreduced attrition.

EP 511013 A2 provides an improved process for the production of C2-C5olefins from higher olefinic or paraffinic or mixed olefin and paraffinfeedstocks. In accordance with this prior art, the hydrocarbon feedmaterials are contacted with a particular ZSM-5 catalyst at elevatedtemperatures, high space velocity and low hydrocarbon partial pressureto produce lower olefins. The catalysts is treated with steam prior touse in the hydrocarbon conversion. The preferred method is to heat thecatalyst at 500 to 700° C., preferably 550 to 600° C., under 1 to 5atmospheres, preferably 1.5 to 3 atmospheres steam for 1 to 48 hours,preferably 15 to 30 hours. The active catalyst component isphosphorus-containing ZSM-5 having a surface Si/Al ratio in the range20-60. Preferably, the phosphorus is added to the formed ZSM-5 as byimpregnating the ZSM-5 with a phosphorus compound in accordance with theprocedures described, for example, in U.S. Pat. No. 3,972,832. Lesspreferably, the phosphorus compound can be added to the multicomponentmixture from which the catalyst is formed. The phosphorus compound isadded in amount sufficient to provide a final ZSM-5 composition having0.1-10 wt. % phosphorus, preferably 1-3 wt. %.

The phosphorus-containing ZSM-5 is preferably combined with knownbinders or matrices such as silica, kaolin, calcium bentonite, alumina,silica aluminate and the like. The ZSM-5 generally comprises 1-50 wt. %of the catalyst composition, preferably 5-30 wt. % and most preferably10-25 wt. %. There is no introduction of metals such as Ca in thecatalyst. ZSM-5 content is below 50%, there is no presteaming step.

EP 568913 A2 describes a method for preparing a ZSM-5 based catalystadapted to be used in the catalytic conversion of methanol or dimethylether to light olefins, wherein it comprises the following consecutivesteps:

-   -   mixing a zeolite ZSM-5 based catalyst with silica sol and        ammonium nitrate solution,    -   kneading, moulding, drying and calcining the mixture,    -   exchanging the modified zeolite with a solution of HCl at 70-90°        C.,    -   drying and calcining the H-modified zeolite,    -   impregnating the H-modified zeolite with phosphoric acid under        reduced pressure,    -   drying and calcining the P-modified zeolite,    -   impregnating the P-modified zeolite with a solution of rare        earth elements under reduced pressure,    -   drying and calcining the P-rare earths-modified zeolite,    -   hydrothermally treating the P-rare earths-modified zeolite at        500-600° C. with water vapour, and    -   calcining the modified zeolite.

WO 03 020667 relates to a process of making olefin, particularlyethylene and propylene, from an oxygenate feed, comprising contacting anoxygenate feed with at least two different zeolite catalysts to form anolefin composition, wherein a first of the zeolite catalysts contains aZSM-5 molecular sieve and a second of the zeolite catalysts contains azeolite molecular sieve selected from the group consisting of ZSM-22,ZSM-23, ZSM-35, ZSM-48, and mixtures thereof. The ZSM-5 can beunmodified, phosphorus modified, steam modified having a microporevolume reduced to not less than 50% of that of the unsteamed ZSM-5, orvarious mixtures thereof. According to one embodiment, the zeolite ismodified with a phosphorus containing compound to control reduction inpore volume. Alternatively, the zeolite is steamed, and the phosphoruscompound is added prior to or after steaming. The amount of phosphorus,as measured on an elemental basis, is from 0.05 wt. % to 20 wt. %, andpreferably is from 1 wt. % to 10 wt. %, based on the weight of thezeolite molecular sieve. Preferably, the atomic ratio of phosphorus toframework aluminum (i.e. in the zeolite framework) is not greater than4:1 and more preferably from 2:1 to 4:1. Incorporation of a phosphorusmodifier into the catalyst of the invention is accomplished, accordingto one embodiment, by contacting the zeolite molecular sieve eitheralone or the zeolite in combination with a binder with a solution of anappropriate phosphorus compound. The solid zeolite or zeolite catalystis separated from the phosphorus solution, dried and calcined. In somecases, the added phosphorus is converted to its oxide form under suchconditions. Contact with the phosphorus-containing compound is generallyconducted at a temperature from 25° C. to 125° C. for a time from 15minutes to 20 hours. The concentration of the phosphorus in the zeolitemay be from 0.01 wt. % to 30 wt. %. This prior art discloses anon-formulated P-ZSM-5.

WO 2009 022990 A1 describes a catalyst composition for dehydration of analcohol to prepare an alkene. The catalyst composition comprises acatalyst and a modifying agent which is phosphoric acid, sulfuric acidor tungsten trioxide, or a derivative thereof. There is no binder.

EP 2348004 A1 relates to the dehydration of ethanol to make ethylene andconversion of methanol to make a mixture of olefins (MTO). The catalystis made by the following process: A ZSM-5 is steamed, P is introduced bycontacting the steamed zeolite with an H3PO4 solution under refluxconditions, the P modified zeolite is extruded with a binder, calcium isintroduced and the resulting catalyst is steamed two hours at 600° C.This prior art discloses a formulated P-ZSM-5, where at least a part ofphosphorous was introduced into zeolite before formulation step.

WO 2009-098262 A1 relates to the dehydration of ethanol to makeethylene. The catalyst is made by the following process: A ZSM-5 issteamed, P is introduced by contacting the steamed zeolite with an H3PO4solution under reflux conditions, the P modified zeolite is extrudedwith a binder, there is no final steaming. There is no introduction ofcalcium.

EP 2082802 A1 relates to various petrochemical processes, thedehydration of alcohols to make an olefin having the same number ofcarbon atoms as the alcohol is not cited. Among the cited processes arethe cracking of olefins and the conversion of oxygenates, e.g. methanolto make a mixture of ethylene, propylene, butenes and varioushydrocarbons. The catalyst is made by the following process: A ZSM-5 issteamed, the steamed zeolite is extruded with a binder, P is introducedby contacting the steamed zeolite with an H3PO4 solution under refluxconditions, calcium is introduced in form of metal silicate and theresulting catalyst is steamed two hours at 600° C.

U.S. Pat. No. 4,356,338 relates to the aromatization of hydrocarbon, thedehydration of alcohols to make an olefin having the same number ofcarbon atoms as the alcohol is not cited. The zeolite (ZSM-5) may becombined with a binder and is treated by a P containing component orsteam or both steam and P containing component. There is no introductionof metals such as Ca in the catalyst. The said catalyst has a reducedcoking.

It has now been discovered a new process to make P modified zeolites.

Brief description of the invention

The present invention relates, in a first embodiment, to a method tomake a phosphorus modified zeolite comprising the following steps inthis order,

a) providing a zeolite comprising at least one ten members ring in thestructure, optionally steaming said zeolite,b) mixing said zeolite of step a) with at least a component selectedamong one or more binders and shaping additives, then shaping saidmixture,c) optionally making a ion-exchange,d) optionally steaming the shaped catalyst, optionally before step c),at least among said steaming of step d) and the steaming of step a) oneis mandatory,e) introducing phosphorus on the catalyst to introduce at least 0.1 wt %of phosphorus, said introduction being made by dry impregnation orchemical vapor deposition,f) optionally introducing a metal, optionally simultaneously with stepe),g) optionally washing the catalyst,h) optionally calcinating the catalyst,i) steaming the catalyst, also referred to as the equilibration step.

The present invention relates, in a second embodiment, to a method tomake a phosphorus modified zeolite comprising the following steps inthis order,

a) providing a zeolite comprising at least one ten members ring in thestructure, optionally steaming said zeolite,b) mixing said zeolite of step a) with at least a component selectedamong one or more binders and shaping additives, then shaping saidmixture,c) optionally making a ion-exchange,d) optionally steaming the shaped catalyst, optionally before step c),at least among said steaming of step d) and the steaming of step a) oneis mandatory,e) introducing phosphorus on the catalyst to introduce at least 0.1 wt %of phosphorus,f) optionally introducing a metal, optionally simultaneously with stepe),g) optionally washing the catalyst,h) optionally calcinating the catalyst,i) steaming the catalyst, also referred to as the equilibration step, ata steaming severity (X) of at least about 2.The above-described “steaming severity (X)” is an important, measurableand critical definition of treatment conditions for the steps d) whichare useful in the instant invention.

“About” means that it could be slightly under 2. As explained hereunderthe severity describes conditions of steaming to achieve adealumination.

The matter is that the results of the steaming is a function of thenature of catalyst (type of zeolite, type of binder, Si/Al ratio,crystal size, crystallinity, structure defects, the presence of occludedcontaminants etc) as well as of conditions of the treatment used. It isclear that the minimum severity is not an absolute value, consideringthe above parameters it can vary from a catalyst to another. The manskilled in the art can easily determine the minimun severity. To be surehe can, by way of example, extend the duration of treatment and/orincrease the temperature.The critical parameters for the treatment include mainly steam partialpressure, temperature and duration of the treatment. If the objects ofthe treatment were similar nature the effect of the treatment is only afunction of the “steaming severity”.A steaming or a hydrothermal treatment of the zeolite above 500° C.leads to a delumination of the framework. A degree of dealuminationcould be measured by ²⁷Al, ²⁹Si MAS NMR, by acidity measurement (likeTPD NH₃) or by any other means, which are well known in the prior art. Arate of the dealumination is defined mainly by mentioned aboveparameters, namely, steam partial pressure, temperature and duration ofthe treatment.Thus, the “steaming severity (X)” is defined as a ratio of thedealumination rates between an experimental condition vs a standardcondition.Steaming performed at 600° C., in 100% of steam at atmospheric pressureduring 2 h is selected as a standard condition for this invention.The rate of dealumination (V) for the catalyst of invention is given byequation:

V÷Const×P(H₂O)̂1.5×t _(st)/EXP(−0.03×T_(st)),

where P(H₂O)—steam partial pressure (P/Patm); T_(st)—steamingtemperature in ° C.; t_(st)—time in hours (duration) of treatment and ÷means proportional.

X(The steamingseverity)=V_(experimental condition)/V_(standard condition)

This equation is valid in a steaming interval from 500° C. to 760° C.So, the steaming severity value could be achieved even at lowertemperature relative to the used in standard condition but for a highertime of duration.The temperature 625° C. provides roughly 2 times higher steam severityvs the standard condition at equal time steam partial pressure andduration of the treatment.

If the temperature of the equilibration step is above 760° C. (out ofthe range), the duration of steaming is at least 0.1 h and the partialpressure of steam is at least 0.01 bar.

Advantageously in the second embodiment the temperature of theequilibration step is in the range 625 to 870° C.

In an embodiment the shaped zeolite (or molecular sieve) of step b)contains less that 1000 wppm of sodium, less that 1000 wppm of potassiumand less that 1000 wppm of iron.

In an embodiment the shaped zeolite (or molecular sieve) of step b)contains less than 1000 wppm of sodium.

In an embodiment the shaped zeolite (or molecular sieve) of step b)contains less than 100 wppm of sodium

In an embodiment the shaped zeolite (or molecular sieve) of step b)contains less that 100 wppm of sodium, less that 100 wppm of potassiumand less that 500 wppm of iron.

The present invention also relates to the use of the catalyst madeaccording to the above method in processes wherein said catalyst isoperated in presence of steam at high temperature. “High temperature”means above 300° C. and up to 800° C. By way of example one can cite,the alcohol dehydration to convert at least an alcohol into thecorresponding olefin, the olefin cracking to make lighter olefins, theMTO and the alkylation of aromatics by alcohols with olefins and/oralcohols, said process producing, by way of example, para-xylene,ethylbenzenes and cumene.

DETAILED DESCRIPTION OF THE INVENTION

As regards the zeolite of step a) containing at least one 10 membersring into the structure, one can cite the crystalline silicates. It isby way of example the MFI (ZSM-5, silicalite-1, boralite C, TS-1), MEL(ZSM-11, silicalite-2, boralite D, TS-2, SSZ-46), FER (Ferrierite, FU-9,ZSM-35), MTT (ZSM-23), MWW (MCM-22, PSH-3, ITQ-1, MCM-49), TON (ZSM-22,Theta-1, NU-10), EUO (ZSM-50, EU-1), MFS (ZSM-57) and ZSM-48 family ofmicroporous materials consisting of silicon, aluminium, oxygen andoptionally boron.

Preferred zeolite structures are selected from the MFI, MTT, FER, MEL,TON, MWW, EUO, MFS.

In an embodiment, the zeolite is ZSM-5 with Si/Al atomic ratio rangingfrom 11 to 30, which has been made without direct addition of organictemplate.

In an embodiment, the zeolite is MFI zeolite with Si/Al atomic ratioranging from 30 to 200.

The three-letter designations “MFI” and “MEL” each representing aparticular crystalline silicate structure type as established by theStructure Commission of the International Zeolite Association. Examplesof a crystalline silicate of the MFI type are the synthetic zeoliteZSM-5 and silicalite and other MFI type crystalline silicates known inthe art. Examples of a crystalline silicate of the MEL family are thezeolite ZSM-11 and other MEL type crystalline silicates known in theart. Other examples are Boralite D and silicalite-2 as described by theInternational Zeolite Association (Atlas of zeolite structure types,1987, Butterworths). The preferred crystalline silicates have pores orchannels defined by ten oxygen rings.

Crystalline silicates are microporous crystalline inorganic polymersbased on a framework of XO₄ tetrahedra linked to each other by sharingof oxygen ions, where X may be trivalent (e.g. Al, B, . . . ) ortetravalent (e.g. Ge, Si, . . . ). The crystal structure of acrystalline silicate is defined by the specific order in which a networkof tetrahedral units are linked together. The size of the crystallinesilicate pore openings is determined by the number of tetrahedral units,or, alternatively, oxygen atoms, required to form the pores and thenature of the cations that are present in the pores. They possess aunique combination of the following properties: high internal surfacearea; uniform pores with one or more discrete sizes; ionexchangeability; good thermal stability; and ability to adsorb organiccompounds. Since the pores of these crystalline silicates are similar insize to many organic molecules of practical interest, they control theingress and egress of reactants and products, resulting in particularselectivity in catalytic reactions. Crystalline silicates with the MFIstructure possess a bidirectional intersecting pore system with thefollowing pore diameters: a straight channel along [010]:0.53-0.56 nmand a sinusoidal channel along [100]:0.51-0.55 nm. Crystalline silicateswith the MEL structure possess a bidirectional intersecting straightpore system with straight channels along [100] having pore diameters of0.53-0.54 nm.

In an embodiment, the zeolite is pretreated by steam. The pretreatmentis performed in the range 420 to 870° C., more preferably in the range480 to 800° C. The water partial pressure may range from 13 to 100 kPa.The steam atmosphere preferably contains from 5 to 100 vol % steam withfrom 0 to 95 vol % of a gas, preferably nitrogen or air. The steamtreatment is preferably carried out for a period of from 0.01 to 200hours, more preferably from 0.05 to 50 hours, still more preferably forat least 0.1 hour and in a preferred way from 0.1 to 50 hours and in amore preferred way from 0.5 to 50 hours and still more preferred 1 to 50hours.

The steam treatment tends to reduce the amount of tetrahedral aluminiumin the crystalline silicate framework by forming alumina. Preferably,the amount of residual tetrahedral Al in the zeolite is between 60 to95%. This value can be estimated by ²⁷Al MAS NMR or TPD NH3. Optionallysaid alumina can be removed by leaching with an acid.

In an embodiment, the ZSM-5 with Si/Al atomic ratio ranging from 11 to30, which has been made without direct addition of organic template, ispretreated by steam.

Additionally, if during the preparation of the zeolite alkaline oralkaline earth metals have been used, the molecular sieve might besubjected to an ion-exchange step. Conventionally, ion-exchange is donein aqueous solutions using ammonium salts or inorganic acids.

In an embodiment, the zeolite is subjected to dealumination such asabout 10% by weight of the aluminium is removed. Such dealumination canbe done by any conventional techniques known per se but isadvantageously made by a steaming optionally followed by a leaching. Thecrystalline silicate having a ratio Si/Al of at least about 30 to 200can be synthetized as such or it can be prepared by dealumination of acrystalline silicate with lower initial Si/Al ratio.

As regards step b), and the binder, it is selected so as to be resistantto the temperature and other conditions employed in the processes usingthe catalyst. The binder can be an inorganic material selected fromsilica, zirconia, borates, alumina, silica-aluminas, phosphates, forexample amorphous aluminophosphates, calcium phosphates, clays, metaloxides such as Zr0₂ and/or metals, or gels including mixtures of silicaand metal oxides.

In an embodiment, the binder is substantially neutral (inert) and it isselected from inorganic material selected from silica, non-acid alumina,amorphous aluminophosphates, metalphosphates, clays or a mixture ofthereof. The neutral nature of the binder allow limiting secondaryreactions leading to formation of heavy oxygenates and hydrocarbons,etane, acetaldehyde etc.

A particularly preferred binder for the catalyst of the presentinvention comprises silica. The relative proportions of the finelydivided crystalline silicate material and the inorganic oxide of thebinder can vary widely.

Non-limiting examples of silicon sources include silicates, precipitatedsilicas, for example, Zeosil range available from Rhodia, fumed silicas,for example, Aerosil-200 available from Degussa Inc., New York, N.Y.,silicon compounds such as tetraalkyl orthosilicates, for example,tetramethyl orthosilicate (TMOS) and tetraethylorthosilicate (TEOS),colloidal silicas or aqueous suspensions thereof, for exampleLudox-HS-40 sol available from E.I. du Pont de Nemours, Wilmington,Del., silicic acid, alkali-metal silicate, or any combination thereof.

Other suitable forms of amorphous silica include silica powders, such asUltrasil VN3SP (commercially available from Degussa).

Other non-limiting examples of a suitable solid silica source arespecial granulated hydrophilic fumed silicas, mesoporous silica gradeEXP & high surface area precipitated silica SIPERNAT from Evonik, HiSil233 EP (available from PPG Industries) and Tokusil (available fromTokuyama Asia Pacific).

In addition, suitable amorphous silica sources include silica sols,which are stable colloidal dispersions of amorphous silica particles inan aqueous or organic liquid medium, preferably water.

Non-limiting examples of commercially available silica sols includethose sold under the tradenames Nyacol (available from Nyacol NanoTechnologies, Inc. or PQ Corp.), Nalco (available from Nalco ChemicalCompany), Ultra-Sol (available from RESI Inc), Ludox (available fromW.R. Grace Davison), NexSil (available from NNTI).

Many silica sols are prepared from sodium silicate and inevitablycontain sodium. It is, however, found that the presence of sodium ionscan cause sintering of the silica body at high temperature and/or affectcatalytic performance. Therefore, if silica sols containing sodium areused, a step of ion exchange may be required in order to reduce orremove sodium. To avoid carrying out ion exchange steps, it isconvenient to use silica sols that contain very little or, ideally, nodetectable traces of sodium and have a pH value of less than 7. Mostpreferably, the silica sol used in the process is slightly acidic withor without polymeric stabilizers. Non limiting examples of silica solsthat contain no detectable traces of sodium include Bindzil 2034DI,Levasil 200, Nalco 1034A, Ultra-Sol 7H or NexSil 20A.

In some case, silica dispersion prepared with alkylammonium might beuseful. Non-limiting examples of commercially low sodium silica solsstabilized by ammonia or alkylammonium cations include LUDOX TMA(available from W.R. Grace Davison) or VP WR 8520 from Evonik.

The silica sols with higher SiO2 content than 30% and even up to 50 wt%, for example W1250, W1836, WK341, WK7330 from Evonik are particularlypreferred.

The preferred source of silicon is a silica sol or a combination ofsilica sol with precipitated or fumed silica.

Types of silica sols used to form a bound catalyst for use in alcoholdehydration process are commercially available as aquasols or organosolscontaining dispersed colloidal silica particles. For example, sodiumsilicate can be used as a silica sol. Otherwise, a silica gel, fumed orpyrogenic silica may also be used to provide a silica binder in themolecular sieve catalyst. Silicic acid is another possible source ofsilica. Advantageously, the binder contains low amount of sodium below1000 ppm.

Clays are known to be essentially inert under a wide range of reactionconditions. Suitable clays include commercially available products suchas kaolin, kaolinite, montmorillonite, attapulgite, saponite, andbentonite. These clays can be used as mined in their natural state, orthey may also be employed in highly active forms, typically activated byan acid treatment procedure. Commercial suppliers of these clays includeThiele Kaolin Company, American Colloidal Co., and others.

Clays contribute to strength as a binder enhancing the attritionresistance properties of the catalyst particles, and clays incombination with binders contribute to the hardness of the particles.Clays also start as small particles and have a higher density, such thatwhen combined with the molecular sieve and binder provide for denserparticles, imparting the desirable characteristic of higher density.

Clays are used in this process to form a hardened product include, butare not limited to, kaolin, kaolinite, montmorillonite, saponite,bentonite, and halloysite.

In an embodiment, the binder material is often, to some extent, porousin nature and may be effective to promote the desired conversion ofethanol to ethylene. The binder might be a single amorphous entity, or ablend of two or more individual amorphous compounds.

In a related embodiment, the catalyst (zeolite+binder) has a volume ofthe pore between 30 Å and 1000 Å of at least 0.25 cc/g, advantageouslybetween 0.25 and 1 cc/g preferably at least 0.26 cc/g, the mostpreferable between 0.27-0.92 cc/g. “cc” means cm³.

In an embodiment, the binder material possesses acid properties and mayalso promote conversion of the ethanol.

In referring to these types of binders that may be used, it should benoted that the term silica-alumina does not mean a physical mixture ofsilica and alumina but means an acidic and amorphous material that hasbeen cogelled or coprecipitated. This term is well known in the art andis described, for example, in U.S. Pat. No. 3,909,450 BI; U.S. Pat. No.3,274,124 B1 and U.S. Pat. No. 4,988,659 BI. In this respect, it ispossible to form other cogelled or coprecipitated amorphous materialsthat will also be effective as either binder or filler materials. Theseinclude silica-zirconias, silica-thorias, silica-berylias,silica-titanias, silica-alumina-thofias, silica-alumina-zirconias,alurninophosphates, mixtures of these, and the like.

In another embodiment, catalyst contains alumina materials such asaluminum oxyhydroxide, γ-alumina, boehmite, diaspore, and transitionalaluminas such as α-alumina, β-alumina, γ-alumina, δ-alumina, ε-alumina,κ-alumina, and ρ-alumina, aluminum trihydroxide, such as gibbsite,bayerite, nordstrandite, doyelite, and mixtures thereof.

It is desirable to provide a catalyst having a good crush strength. Thisis because in commercial use, it is desirable to prevent the catalystfrom breaking down into powder-like materials. Such oxide binders havebeen employed normally only for the purpose of improving the crushstrength of the catalyst.

The catalyst composition may be prepared, as indicated above, by any ofthe methods described in the art. Advantageously, however, the catalystparticles are combined with the binder material initially by dry-mixing,then in a liquid, preferably water, preferably with a plasticizer, toyield a paste.

As plasticizer (shaping additive), there may be mentioned one that willbe decomposed during any subsequent heat treatment, e.g., calcination.Suitable materials for this purpose include, for example, alkylatedcellulose derivatives, hydroxyethylcellulose (HEC), tylose, ammoniumalginate, polyvinyl pyrrolidone, glycerol, and polyethylene glycol.

In addition to enhancing the catalyst strength properties, the bindermaterial allows the molecular sieve crystallite powder to be bound intolarger particle sizes suitable for commercial catalytic processes. Theformulation of the mixture b) may be formed into a wide variety ofshapes including extrudates, spheres, pills, and the like.

The uniformly mixed paste may subsequently be shaped, for example byspray drying to yield microspheres, pelletizing or, preferably, byextrusion.

The paste is then extruded, for example in a piston extruder, intostrings, for example cylindrical, dried, again calcined, and choppedinto pieces of a desired length.

As regards the proportions of the zeolite, the one or more binders andshaping additives, advantageously the proportion of the zeolite is from5 to 95w % of the catalyst. The catalyst comprises the zeolite and atleast a component selected among one or more binders and shapingadditives. The amount of zeolite which is contained in the catalystranges more advantageously from 15 to 90 weight percent of the totalcatalyst, preferably 20 to 85 weight percent of the catalyst.

Once the molecular sieve catalyst composition is shaped, and in asubstantially dry or dried state, a heat treatment, for examplecalcination, is advantageously performed to harden and/or activate thecomposition. Therefore the heat treatment is preferably carried out at atemperature of at least 400° C., for a period of from 1 to 48 hours.Calcination may be carried out, for example, in a rotary calciner, fluidbed calciner, or a batch oven.

As regards the Ion-exchange of step c), purpose is to get advantageouslya formulated zeolitic molecular sieve with an inert binder, beforesubjecting in a contact with a phosphatation agent, having less than1000 wppm of alkali & alkali-earth metals, Na, K, Fe as well as lessthan 200 ppm of red-ox & noble elements such as Zn, Cr, Rh, Mn, Ni, V,Mo, Co, Cu, Cd, Pt, Pd, Ir, Ru, Re. This may achieved by an optionalback ion-exchange step known per se.

In an embodiment, the catalyst comprises a molecular sieve has beentreated to reduce alkali metal content to less than 100 ppm before orafter the steaming step d).

Although in principle mixing with the binder and ion exchange may becarried out in any order, advantageously ion exchange is performed aftershaping but before phosphorus introduction.

Advantageously, the ion exchange step is performed on shaped calcinedcatalyst before or after the steaming step d).

As regards the steaming of step d), it is also known as the pre-steamingby reference to the final steaming of step i). The treatment isperformed in the range 420 to 870° C., more preferably in the range 480to 800° C. The water partial pressure may range from 13 to 100 kPa. Thesteam atmosphere preferably contains from 5 to 100 vol % steam with from0 to 95 vol % of a gas, preferably nitrogen or air. The steam treatmentis preferably carried out for a period of from 0.01 to 200 hours, morepreferably from 0.05 to 50 hours, still more preferably for at least 0.1hour and in a preferred way from 0.1 to 50 hours and in a more preferredway from 0.5 to 50 hours and still more preferred 1 to 50 hours.

The steam treatment tends to reduce the amount of tetrahedral aluminiumin the crystalline silicate framework by forming alumina. Preferably,the amount of residual tetrahedral Al in the zeolite is between 60 to95%. This value can be estimated by ²⁷Al MAS NMR or TPD NH₃.

As regards the introduction of P of step e), said introduction ofphosphorus can be performed under reduced or atmospheric pressure attemperature from 10 to 400° C. A non-limiting source of phosphorus canbe provided in aqueous or non-aqueous medium.

In an embodiment, the non-aqueous medium is selected from the groupcontaining ethanol, methanol or other alcohols.

The preferred techniques are impregnation and chemical vapourdeposition. Said techniques are mandatory in the first embodiment of theinvention.

These techniques imply a minimum waste to treat and allow maintainingsubstantially all phosphorus on the catalyst.

In an embodiment, the catalyst precursor is treated by a source ofphosphorus injected into a steam flow. In this case, the phosphatationis performed under mild steaming condition with a steam flow containingphosphorus at 100-400° C.

In an embodiment, the phosphorus is introduced by a treatment of thecatalyst precursor (zeolite+binder) in a solution containing a source ofphosphorus at temperature 25-100° C. for 0.1-96 h followed by filteringor evaporation.

In an embodiment amount of said acid solution containing P isadvantageously between 2 and 10 liters per kg of zeolite plus binder. Atypical period is around 0.5 to 24 hours. Advantageously the aqueousacid solution containing the source of P has a pH of 3, advantageously2, or lower. Advantageously said aqueous acid solution is phosphorusacids, a mixture of phosphorus acids and organic or inorganic acid ormixtures of salts of phosphorus acids and organic or inorganic acids.The phosphorus acids or the corresponding salts can be of the phosphate([PO₄]³⁻, being tribasic), phosphite ([HPO₃]²⁻, being dibasic), orhypophosphite ([H₂PO₂]¹⁻, being monobasic), type. Of the phosphate typealso di or polyphosphates ([P_(n)O_(3n+1)]^((n+2)−)) can be used. Thecontact of the zeolite+binder with the P containing component can bemade under reflux conditions.

In a preferred embodiment the incipient wetness impregnation techniqueis used. In this case the phosphorus is introduced via impregnationusing a limited amount of liquid water which is subjected to a contactwith catalyst. This method is also known as the dry impregnation.

Incipient wetness (IW) or incipient wetness impregnation (IWI) is acommonly used technique for the synthesis of heterogeneous catalysts.Typically, the precursor (phosphorus-containing compounds) is dissolvedin an aqueous or organic solution. The volume of solution, which is usedfor dissolution of the precursor, is substantially the same as the porevolume of catalyst precursor containing both binder and zeolite. Thenthe precursor-containing solution is added to a catalyst precursor.Capillary action draws the solution into the pores. The catalyst canthen be dried and calcined to drive off the volatile components withinthe solution, depositing the phosphorus on the catalyst surface.

The sample before impregnation can be dried or calcined. Theimpregnation could be performed at room or elevated temperature (30-100°C.).

The adsorption capacity is typically measured by impregnating the driedextruded zeolite with water until the zeolite was completely wet.Weighing the zeolite before and after impregnation gives the absorptioncapacity:

${{Absorption}\mspace{14mu} {capacity}\mspace{14mu} (\%)} = {\frac{{{weight}\mspace{14mu} {after}\mspace{14mu} {impregnation}} - {{dry}\mspace{14mu} {weight}}}{{dry}\mspace{14mu} {weight}}*100}$

In an embodiment, H3PO4 solution is used for impregnation.

Advantageously, a mixture of H3PO4 with their ammonium salts providing apH of the aqueous solution higher than 2.0 is used for impregnation

In an embodiment, the sources of phosphorus are substantially metal freecomponents, for example H3PO4, ammonium phosphates or organicP-compounds. “substantially metal free” means a metal proportion withhas no adverse effect on the P introduction. By way of example thisproportion can be below 1000 wppm.

The amount of phosphorus on the catalyst can be from 0.5 to 30 wt %, butpreferably from 0.5 to 9 w %.

In an embodiment, the phosphatation step is performed before orsimultaneously with introduction of metal oxides.

As regards step f), the introduction of metal, it can be one or moremetals. Advantageously said metals are selected among alkaline earth orrare earth metals. The alkaline earth or rare earth metal M ispreferably selected from one or more of: Mg, Ca, Sr, Ba, La, Ce. Morepreferably, M is an alkaline earth metal. Most preferably, M is Ca.Particularly in the case of P-modification via steaming and leaching, Mcan be a rare earth metal such as La and Ce. Advantageously the metal isintroduced in a soluble form.

The M-containing component is preferably in the form of an organiccompound, a salt, hydroxide or oxide. The compound is preferably in asolubilized form when bringing it into contact with the molecular sieve.Alternatively, the solution of the M-containing compound can be formedafter bringing the molecular sieve in contact with said compound.

Possible M-containing compounds include compounds such as sulphate,formate, nitrate, acetate, halides, oxyhalides, oxalate, borates,carbonate, hydroxide, oxide and mixtures thereof. One can cite calciumcarbonate.

Those M-containing compounds, which are poorly water-soluble, can bedissolved to form a well-solubilized solution by heating and/or bymodifying the pH of the solution by addition of phosphoric, acetic ornitric acid or corresponding ammonium salts of said acids.

As regards step g), a washing step can be envisaged. In accordance withthe present invention, the catalyst is treated with water for a periodof time from 0.1 to 48 hours, preferably for a period of time from about0.5 to 36 hours and most preferably from about 1 to 24 hours. The waterwas at a temperature between about 20° C. and 180° C., preferablybetween about 20° C. and 100° C. and most preferably between about 25°C. and 60° C. By way of example the water can be at 30° C. Following thewater treatment, the catalyst may be dried at about >60° C. Optionally,the water can contain at least one dissolved solid selected from thegroup consisting of ammonium chloride, ammonium phosphate, ammoniumsulfate, ammonium acetate, ammonium carbonate, ammonium nitrate andmixtures thereof.

As regards step h), said calcination can be made in air or an inert gas,typically at a temperature of from 350 to 900° C. for a period of from 1to 48 hours. Optionally the air or an inert gas may contain steam inconcentration from 10 to 90 vol %.

As regards step i), in the first embodiment of the invention it can beperformed in the range 420 to 870° C., preferably in the range 480 to870° C., preferably from 625 to 870° C. and more preferably from 700 to800° C., still more preferably in the range 720 to 800° C. Alternativelyit can be performed in the range 420 to 600° C., preferably 420 to 580°C.

In the second embodiment of the invention it is performed by steamingsteaming severity above about 2 or alternatively at temperature above625° C., preferably from 625 to 870° C. and more preferably from 700 to800° C. still more preferably in the range 720 to 800° C. The waterpartial pressure may range from 13 to 100 kPa. The steam atmospherepreferably contains from 5 to 100 vol % steam with from 0 to 95 vol % ofa gas, preferably nitrogen or air. The steam treatment is preferablycarried out for a period of from 0.01 to 200 hours, preferably from 0.05to 50 hours, more preferably for at least 0.1 hour and in a preferredway from 0.1 to 50 hours, and in a more preferred way from 0.5 to 50hours and still more preferred 1 to 50 hours.

As regards the dehydration process to convert an alcohol into an olefin,this process has been described in a lot of patent applications. One cancite WO/2009/098262, WO/2009/098267, WO/2009/098268 and WO 2009/098269,the content of which is incorporated in the present application. Thealcohol is any alcohol provided it can be dehydrated to thecorresponding olefin. Advantageously the alcohol has two or more carbonatoms. The corresponding olefin is an olefin having the same number ofcarbons as the alcohol. By way of example mention may be made ofalcohols having from 2 to 10 carbon atoms. Advantageously the inventionis of interest for ethanol, propanol, butanol and phenylethanol.

As regards the cracking of olefins, more precisely the present inventionrelates to a process for cracking an olefin-rich hydrocarbon feedstockwhich is selective towards light olefins in the effluent. In particular,olefinic feedstocks from refineries or petrochemical plants can beconverted selectively so as to redistribute the olefin content of thefeedstock in the resultant effluent. Said cracking of an olefin-richfeedstock is often referred in the following description and claims asOCP (Olefin Cracking Process). As regards the hydrocarbon feedstockcontaining one or more olefins sent to the OCP reactor, in accordancewith the present invention, cracking of olefins is performed in thesense that olefins in a hydrocarbon stream are cracked into lighterolefins and selectively into propylene. The feedstock and effluentpreferably have substantially the same olefin content by weight.Typically, the olefin content of the effluent is within ±15 wt %, morepreferably ±10 wt %, of the olefin content of the feedstock. Thefeedstock may comprise any kind of olefin-containing hydrocarbon stream.The feedstock may typically comprise from 10 to 100 wt % olefins andfurthermore may be fed undiluted or diluted by a diluent, the diluentoptionally including a non-olefinic hydrocarbon. In particular, theolefin-containing feedstock may be a hydrocarbon mixture containingnormal and branched olefins in the carbon range C₄ to C₁₀, morepreferably in the carbon range C₄ to C₆, optionally in a mixture withnormal and branched paraffins and/or aromatics in the carbon range C₄ toC₁₀. Typically, the olefin-containing stream has a boiling point of fromaround −15 to around 180° C. With regards to the OCP process, saidprocess is known per se. It has been described in EP 1036133, EP1035915, EP 1036134, EP 1036135, EP 1036136, EP 1036138, EP 1036137, EP1036139, EP 1194502, EP 1190015, EP 1194500 and EP 1363983 the contentof which are incorporated in the present invention.

As regards the MTO, said process produces light olefins such as ethyleneand propylene as well as heavy hydrocarbons such as butenes. Said MTOprocess is the conversion of methanol or dimethylether by contact with amolecular sieve which can be a P modified zeolite.

As regards the alkylation of aromatic compounds with olefins andalcohols, said process produces, by way of example, para-xylene,ethylbenzenes and cumene. Alkylation of aromatic, for example, toluenemethylation has been known to occur over acidic catalyst, particularlyover zeolite or zeolite-type catalyst. In particular, ZSM-5-typezeolite, zeolite Beta and silicaaluminophosphate (SAPO) catalysts havebeen used for this process.

One skilled in the art will also appreciate that the olefins made by thedehydration process of the present invention can be, by way of example,polymerized. When the olefin is ethylene it can be, by way of example,

polymerized to form polyethylenes,

dimerized to butene and then isomerised to isobutene, said isobutenereacting with ethanol to produce ETBE,

dimerized to butane followed by reacting with ethylene via methatesis toproduce propylene;

converted to propylene over metal, acid or bifunctional catalyst, usedfor alkylation of benzene to form ethyl-benzene,

dimerised to 1-butene, trimerised to 1-hexene or tetramerised to1-octene, said alpha-olefins comonomers are further reacted withethylene to produce polyethylene

dimerised to 1-butene, said 1-butene is isomerised to 2-butene and said2-butene is further converted with ethylene by metathesis reaction intopropylene and said propylene can be polymerised to polypropylene,

converted to ethylene oxide and glycol or

converted to vinyl chloride.

The present invention relates also to said polyethylenes, polypropylene,propylene, butene, hexane, octene, isobutene, ETBE, vinyl chloride,ethylene oxide and glycol.

When the olefin is propylene it can be, by way of example,

polymerized to form polypropylene,

used for alkylation of aromatics etc. . . . .

EXAMPLES Example 1

A sample of zeolite ZSM-5 (Si/Al=12) in NH4-form (contained 250 ppm ofNa & synthesized without template) was blended with a silica binder in aratio 80:20 followed by addition of extrusion additives and shaping. Afinal Na content in the catalyst was 320 ppm.

The extruded sample was dried for 2 h at 140° C., calcined for 2 h at600° C. followed by steaming at 550° C. for 6 h in 100% steam.

Steamed solid was incipient wetness impregnated with an aqueous solutionof phosphoric acid to introduce about 3 wt % of phosphorus to thecatalyst. The impregnated solid was dried for 16 h at 110° C.

Then, the phosphated sample was incipient wetness impregnated with asolution of calcium nitrate obtained by dissolution of calcium carbonateto introduce about 1 wt % of calcium to the solid. The impregnated solidwas dried for 16 h at 110° C.

Resulted catalyst containing 2.8 wt % of phosphorus and 0.8% of calciumwas steamed at 600° C. for 2 h in 100% of steam (steaming severity 1).The sample is hereinafter identified as sample A.

Resulted catalyst containing about 2.8 wt % of phosphorus and 0.8% ofcalcium was steamed at 750° C. for 1 h in 100% of steam (steamingseverity 45). The sample is hereinafter identified as sample B. Totalpore volume measured by mercury intrusion porosimetry is 0.36 cm3/g.

Catalyst tests were performed on 1 ml of catalyst grains (35-45 meshes)loaded in a tubular reactor with internal diameter 11 mm. A mixture 25wt % EthOH/75 wt % H₂O was subjected to a contact with catalystdescribed in the example I in a fixed bed reactor at 380° C., WHSV=7 h⁻¹P=2 bara. The results are given in table 1 hereunder. The values are theweight percents on carbon basis.

Example 2

A sample of zeolite ZSM-5 (Si/Al=12) in NH4-form (containing 250 ppm ofNa & synthesized without template) was blended with a silica binder in aratio 80:20 followed by addition of extrusion additives and shaping. Afinal Na content in the catalyst was 320 ppm.

The extruded sample was dried for 16 h at 110° C., calcined for 10 h at600° C. followed by steaming at 550° C. for 6 h in 100% steam.

Steamed shaped zeolite was then contacted with an aqueous solution ofH₃PO₄ (85% wt) under conditions of incipent wetness. Then 1 g of CaCO₃was introduced. After stirring during 30 min, the system is cooled downat room temperature and the excess of solution is removed by filtrationwithout washing. The recovered solid is dried at 110° C. for 16 hfollowed by steaming at 600° C. for 2 h in 100% of steam (steamingseverity 1).

Resulted catalyst contained about 1.7 wt % of phosphorus and 0.4 wt % ofcalcium. The sample is hereinafter identified as sample C

The performances of the catalyst were then evaluated under the sameoperating conditions as described above, using 1 ml of catalyst (35-45mesh) loaded in a tubular reactor with internal diameter 11 mm. Amixture of 25 wt % EtOH/75 wt % H₂O has been processed on catalyst C, ina fixed bed reactor at 380° C., WHSV=7 h⁻¹ P=2 bara. The results aregiven in table 1. The values are the weight percents on carbon basis.

Example 3

A sample of zeolite ZSM-5 (Si/Al=12) in NH4-form (containing 250 ppm ofNa & synthesized without template) was blended with a silica binder in aratio 80:20 followed by addition of extrusion additives and shaping. Afinal Na content in the catalyst was 320 ppm.

The extruded sample was dried for 16 h at 110° C., calcined for 10 h at600° C. followed by steaming at 550° C. for 6 h in 100% steam.

12 g of steamed solid was incipient wetness impregnated with an aqueoussolution containing 1.54 g of NH4H2PO4. The impregnated solid was driedfor 16 h at 110° C.

Then, the phosphated sample was incipient wetness impregnated with asolution of calcium nitrate obtained by dissolution of 0.3 g calciumcarbonate in nitric acid. The impregnated solid was dried for 16 h at110° C. followed by steaming at 600° C. for 2 h in 100% of steam(steaming severity 1).

Resulted catalyst contained about 2.54 wt % of phosphorus and 0.82 wt %of calcium. The sample is hereinafter identified as sample D.

The performances of the catalyst were then evaluated under the sameoperating conditions as described above, using 1 ml of catalyst (35-45mesh) loaded in a tubular reactor with internal diameter 11 mm. Amixture of 25 wt % EtOH/75 wt % H₂O has been processed on catalyst D, ina fixed bed reactor at 380° C., WHSV=7 h⁻¹ P=2 bara. The results aregiven in table 1. The values are the weight percents on carbon basis.

TABLE 1 Sample A B C D P (bara) 2 2 2 2 T (° C.) 380 380 380 380 WHSV(H-1) 7 7 7 7 EtOH conversion 99.9 99.8 99.9 99.9 (% wt CH2) DEE 0.0 0.00.0 0.0 Acetaldyde 0.31 0.17 0.17 0.13 EtOH 0.10 0.20 0.05 0.05 Yeild onC-basis (% wt CH2) CH4 0.00 0.00 0.00 0.00 C2 0.13 0.06 0.11 0.12 C2=97.9 99.0 97.3 97.4 C3= 0.56 0.07 0.7 0.8 C4+ olef 0.86 0.48 1.6 1.4Unknown 0.10 0.06 0.07 0.08 Selectivity on C-basis (% wt CH2) C2= 98.099.20 97.4 97.4 C2's cut purity (%) 99.87 99.94 99.88 99.87

Example 4

A sample of zeolite ZSM-5 (Si/Al=12) in NH4-form (contained 250 ppm ofNa & synthesized without template) was blended with a binder containingsilica and kaolin in a ratio 70:10:20 followed by addition of extrusionadditives and shaping.

The extruded sample was dried for 2 h at 140° C., calcined for 10 h at600° C. followed by steaming at 550° C. for 6 h in 100% steam.

Steamed solid was incipient wetness impregnated with an aqueous solutionof phosphoric acid to introduce about 3 wt % of phosphorus to thecatalyst. The impregnated solid was dried for 16 h at 110° C.

Then, the phosphated sample was incipient wetness impregnated with asolution of calcium nitrate obtained by dissolution of calcium carbonateto introduce about 1 wt % of calcium to the solid. The impregnated solidwas dried for 16 h at 110oC.

Resulted catalyst containing 2.94 wt % of phosphorus and 0.8% of calciumwas steamed at 750° C. for 2 h in 100% of steam (steaming severity 90).The sample is hereinafter identified as sample E.

Example 5

A sample of zeolite ZSM-5 (Si/Al=12) in NH4-form (synthesized withouttemplate) was calcined for 10 h at 600° C. followed by steaming at 550°C. for 6 h in 100% steam.

100 g of steamed solid was incipient wetness impregnated (dryimpregnated) with an aqueous solution containing 9.86 g of phosphoricacid. The impregnated solid was dried for 16 h at 110° C.

Then, 16 g of the phosphated sample was extruded with 4 g of silicabinder and 0.4 g of CaCO₃.

The resulted catalyst was calcined at 600° C. for 10 h followed bysteaming at 600oC for 2 h in 100% of steam (steaming severity 1). Thesample is hereinafter identified as sample F.

Example 6 OCP Test

Catalyst tests were performed on 0.8 g of catalyst grains (35-45 meshes)loaded in the tubular reactor. The feedstock which containssubstantially non cyclic olefins C4 (˜60%) was subjected to catalyticcracking in the presence of catalyst in a fixed bed reactor atT_(in)-550° C., WHSV=16 h⁻¹, P=1.5 bara. The results are in table 2. Thevalues in the table 2 are the average catalyst performance for 1-10hours-on-stream given in weight percents on carbon basis.

The data given below illustrate good cracking activity and highselectivity of the P-zeolite in C4 olefins conversion to propylene andethylene.

TABLE 2 Sample E F P (bara) 1.5 1.5 T_(in) (° C.) 550 550 WHSV (h⁻¹) 1616 C4 olefins conversion, % 65.4 65.2 Purity C3's, % 94.9 96.0 Yield onC-basis, % Methane 0.07 0.14 Aromatics 1.2 1.4 Propane 1.0 0.8 Ethylene3.5 3.4 Propylene 19.5 19.1

1-29. (canceled)
 30. A method to make a phosphorus modified zeolitecomprising: a) providing a zeolite comprising at least one ten memberring in the structure thereof, and optionally steaming the zeolite; b)mixing the zeolite of step a) with at least a component selected amongone or more binders and shaping additives, and then shaping the mixture;c) optionally making a ion-exchange; d) optionally steaming the shapedmixture, optionally before step c), wherein at least one of the steamingof step d) and the steaming of step a) is mandatory; e) introducingphosphorus on the catalyst to introduce at least 0.1 wt % of thephosphorus, wherein the introduction is made by dry impregnation orchemical vapor deposition; f) optionally introducing a metal, optionallysimultaneously with step e); g) optionally washing the catalyst; h)optionally calcinating the catalyst; i) steaming the catalyst.
 31. Themethod of claim 30, wherein the phosphorus introduction of step e) ismade by incipient wetness (IW) or incipient wetness impregnation (IWI).32. The method of claim 30, wherein the steaming of step i) is performedat a temperature ranging from 420 to 870° C.
 33. The method of claim 30,wherein the steaming of step i) is performed at a temperature rangingfrom 480 to 870° C.
 34. The method of claim 30, wherein the steaming ofstep i) is performed at a temperature ranging from 625 to 870° C. 35.The method of claim 30, wherein the steaming of step i) is performed ata temperature ranging from 700 to 800° C.
 36. The method of claim 30,wherein the steaming of step i) is performed at a temperature rangingfrom 720 to 800° C.
 37. The method of claim 30, wherein the steaming ofstep i) is performed at a temperature ranging from 420 to 600° C. 38.The method of claim 30, wherein the steaming of step i) is performed ata temperature ranging from 420 to 580° C.
 39. The method of claim 30,wherein the shaped zeolite of step b) contains less than 100 wppm ofsodium.
 40. The method of claim 30, wherein the shaped zeolite of stepb) contains less than 100 wppm of sodium, less than 100 wppm ofpotassium and less than 500 wppm of iron.
 41. The method of claim 30,wherein the shaped zeolite of step b) contains less than 1000 wppm ofsodium.
 42. The method of claim 30, wherein the shaped zeolite of stepb) contains less than 1000 wppm of sodium, less than 1000 wppm ofpotassium and less than 1000 wppm of iron.
 43. The method of claim 30,wherein the zeolite is MFI, MTT, FER, MEL, TON, MWW, EUO, or MFS. 44.The method of claim 30, wherein the zeolite is ZSM-5 with Si/Al atomicratio ranging from 11 to 30, and wherein the zeolite has been madewithout direct addition of organic template.
 45. The method of claim 30,wherein the zeolite is MFI with Si/Al atomic ratio ranging from 30 to200.
 46. The method of claim 30, wherein the amount of phosphorus on thecatalyst is from 0.5 to 30 wt %.
 47. The method of claim 46, wherein theamount of phosphorus on the catalyst is from 0.5 to 9 w %.
 48. Themethod of claim 30, wherein the metal at step f) is an alkaline earth orrare earth metal M.
 49. The method of claim 48, wherein the metal is Mg,Ca, Sr, Ba, La, Ce, or combinations thereof.
 50. The method of claim 30,wherein the catalyst has a volume of pores between 30 Å and 1000 Å of atleast 0.25 cc/g.
 51. A method comprising using the catalyst madeaccording the method of claim 30 in a process, wherein the catalyst isoperated in the presence of steam at temperature above 300° C. and up to800° C.
 52. A process comprising dehydrating an alcohol to convert atleast said alcohol into a corresponding olefin having the same number ofcarbon atoms as the alcohol, wherein the dehydration is made in thepresence of the catalyst made according to the method of claim
 30. 53. Aprocess comprising cracking olefins to make lighter olefins, wherein thecracking performed in the presence of the catalyst made according to themethod of claim
 30. 54. A process comprising cracking of methanol ordimethylether to produce light olefins, wherein the cracking isperformed in the presence of the catalyst made according to the methodof claim
 30. 55. The process of claim 54, wherein the light olefinscomprise ethylene and propylene.
 56. A process comprising alkylation ofaromatics by alcohols or olefins, wherein the alkylation is performed inthe presence of the catalyst made according to the method of claim 30.57. A method to make a phosphorus modified zeolite comprising: a)providing a zeolite comprising at least one ten member ring in thestructure thereof, and optionally steaming the zeolite; b) mixing thezeolite of step a) with at least a component selected among one or morebinders and shaping additives, and then shaping the mixture; c)optionally making a ion-exchange; d) optionally steaming the shapedmixture, optionally before step c), wherein at least one of the steamingof step d) and the steaming of step a) is mandatory; e) introducingphosphorus on the catalyst to introduce at least 0.1 wt % of thephosphorus; f) optionally introducing a metal, optionally simultaneouslywith step e); g) optionally washing the catalyst; h) optionallycalcinating the catalyst; i) steaming the catalyst at a steamingseverity (X) of at least about
 2. 58. The method of claim 57, whereinthe steaming of step i) is performed at a temperature ranging from 625to 870° C.
 59. The method of claim 57, wherein the steaming of step i)is performed at a temperature ranging from 700 to 800° C.
 60. The methodof claim 57, wherein the steaming of step i) is performed at atemperature ranging from 720 to 800° C.
 61. The method of claim 57,wherein the shaped zeolite of step b) contains less than 100 wppm ofsodium.
 62. The method of claim 57, wherein the shaped zeolite of stepb) contains less than 100 wppm of sodium, less than 100 wppm ofpotassium and less than 500 wppm of iron.
 63. The method of claim 57,wherein the shaped zeolite of step b) contains less than 1000 wppm ofsodium.
 64. The method of claim 57, wherein the shaped zeolite of stepb) contains less than 1000 wppm of sodium, less than 1000 wppm ofpotassium and less than 1000 wppm of iron.
 65. The method of claim 57,wherein the zeolite is MFI, MTT, FER, MEL, TON, MWW, EUO, or MFS. 66.The method of claim 57, wherein the zeolite is ZSM-5 with Si/Al atomicratio ranging from 11 to 30, and wherein the zeolite has been madewithout direct addition of organic template.
 67. The method of claim 57,wherein the zeolite is MFI with Si/Al atomic ratio ranging from 30 to200.
 68. The method of claim 57, wherein the amount of phosphorus on thecatalyst is from 0.5 to 30 wt %.
 69. The method of claim 57, wherein theamount of phosphorus on the catalyst is from 0.5 to 9 w %.
 70. Themethod of claim 57, wherein the metal at step f) is an alkaline earth orrare earth metal M.
 71. The method of claim 57, wherein the metal is Mg,Ca, Sr, Ba, La, Ce, or combinations thereof.
 72. The method of claim 57,wherein the catalyst has a volume of pores between 30 Å and 1000 Å of atleast 0.25 cc/g.
 73. A method comprising using the catalyst madeaccording the method of claim 57 in a process, wherein the catalyst isoperated in the presence of steam at temperature above 300° C. and up to800° C.
 74. A process comprising dehydrating an alcohol to convert atleast said alcohol into a corresponding olefin having the same number ofcarbon atoms as the alcohol, wherein the dehydration is made in thepresence of the catalyst made according to the method of claim
 57. 75. Aprocess comprising cracking olefins to make lighter olefins, wherein thecracking performed in the presence of the catalyst made according to themethod of claim
 57. 76. A process comprising cracking of methanol ordimethylether to produce light olefins, wherein the cracking isperformed in the presence of the catalyst made according to the methodof claim
 57. 77. The process of claim 76, wherein the light olefinscomprise ethylene and propylene.
 78. A process comprising alkylation ofaromatics by alcohols or olefins, wherein the alkylation is performed inthe presence of the catalyst made according to the method of claim 57.